Highly stable heavy hydrocarbon hydrodesulfurization catalyst and methods of making and use thereof

ABSTRACT

Described is a catalyst useful in the hydroprocessing of a heavy hydrocarbon feedstock wherein the catalyst comprises a calcined mixture made by calcining a formed particle of a mixture comprising molybdenum trioxide, a nickel compound, and an inorganic oxide material. The catalyst may be made by mixing an inorganic oxide material, molybdenum trioxide, and a nickel compound to form a mixture that is formed into a particle and calcined to provide a calcined mixture. The process involves the hydrodesulfurization and hydroconversion of a heavy hydrocarbon feedstock which process may include the conversion of a portion of the pitch content of the heavy hydrocarbon feedstock and the yielding of a treated product having an enhanced stability as reflected by its P-value.

This is a divisional application of U.S. application Ser. No.11/832,461, filed Aug. 1, 2007, which claims the benefit of U.S.Provisional Application Ser. No. 60/821,341, filed Aug. 3, 2006.

BACKGROUND OF THE INVENTION

This invention relates to a catalyst, a method of making a catalyst anda process for making a hydrocarbon product having a low sulfurconcentration. The invention further relates to a highly stable catalystthat is useful in the hydrodesulfurization of a heavy hydrocarbonfeedstock, a method of making a highly stable catalyst for use in thehydrodesulfurization of a heavy hydrocarbon feedstock, and a process forthe hydrodesulfurization of a heavy hydrocarbon product.

One process that is recognized by those skilled in the art ofhydrocarbon hydroprocessing is the hydroconversion of heavy hydrocarbonfeedstocks that contain hydrocarbons boiling above about 538° C. (1000°F.) so as to convert a portion of the heavy hydrocarbons into lighterhydrocarbons. It may also be desirable to simultaneously provide for thereduction of the sulfur content of such heavy hydrocarbon feedstocks.Many of the conventional catalysts used to provide for thehydroconversion and desulfurization of heavy hydrocarbon feedstockscontain a Group VIB metal component, such as molybdenum, and a GroupVIII metal component, such as cobalt or nickel, supported on arefractory oxide support.

U.S. Pat. No. 5,827,421 (Sherwood, Jr) discloses a process for thehydroconversion and desulfurization of a heavy hydrocarbon feedstockusing an alumina supported catalyst containing Group VIII and Group VIBmetals and having specifically defined surface and pore characteristics.In its background section, this patent provides an extensive review anddiscussion of the prior art and the therein described catalysts used inthe hydroconversion of heavy hydrocarbon feedstocks such as petroleumresid and other heavy hydrocarbons. This patent does not, however,provide any detail on the use of molybdenum trioxide as a necessarysource of the molybdenum component of a hydroprocessing catalystcomposition that is made by a method that includes the co-mulling of themolybdenum trioxide with an inorganic oxide material and a nickelcompound.

U.S. Pat. No. 5,686,375 (Iyer et al.) mentions hydroprocessing catalyststhat contain underbedded Group VIII metal components with the preferredcatalyst comprising underbedded nickel and an overlayer of molybdenum.The patent states that many nickel and molybdenum compounds are usefulfor impregnation or comulling including precursors of molybdenumtrioxide, but it does not specifically mention the comulling ofmolybdenum trioxide with the porous refractory support material in thepreparation of its catalyst support that has an underbedded molybdenumcomponent. The patent does, however, mention the incorporation ofmolybdenum onto the support that contains underbedded nickel bycomulling instead of by impregnation. But, there is no teaching in the'375 patent of the preparation of a heavy hydrocarbon hydroconversioncatalyst by the comulling of an inorganic support material with bothmolybdenum trioxide and a nickel compound followed by the resultingmixture being calcined to thereby form a catalyst material.

U.S. Pat. No. 6,030,915 (de Boer) discloses a hydroprocessing catalystthat uses regenerated spent hydroprocessing catalyst fines in themanufacture of a hydroprocessing catalyst. The patent further indicatesthat additional hydrogenation metals may be added to the catalystcomposition by impregnation using an impregnation solution comprisingwater soluble salts of the hydrogenation metals to be incorporated intothe catalyst composition. Also, an alternative method of incorporatingthe extra metal into the catalyst composition is indicated as includingthe mixing of either solid state or dissolved metal components with themixture of regenerated spent hydroprocessing catalyst fines, binder,and, optionally, additive. The solid state metal may include solidmolybdenum oxide. Additives are not indicated as being a catalytic metalcompound. In the preparation of its catalyst, the '915 patent requiresthe regenerated spent hydroprocessing catalyst fines to be mixed with atleast one additive, which may include a binder, such as alumina, silica,silica-alumina, titania and clays.

BRIEF SUMMARY OF THE INVENTION

It is desirable to have a catalyst that has a low production cost andwhich is useful in the hydrodesulfurization of a heavy hydrocarbonfeedstock, such as a crude oil residue, while providing for a conversionof at least a portion of the heavy end of the heavy hydrocarbonfeedstock to lighter hydrocarbons. It is further desirable for thehydrodesulfurized heavy hydrocarbon conversion product resulting fromthe use of the catalyst to exhibit highly stable properties as reflectedby its P-value. It is also desirable for the hydroconversion catalyst toexhibit a low rate of deactivation at the higher temperatures that aretypically required for providing for the conversion of the heavy end ofa heavy hydrocarbon feedstock.

Thus, accordingly, a highly stable heavy hydrocarbonhydrodesulfurization catalyst is provided that comprises a calcinedmixture made by calcining a formed particle of a mixture comprisingmolybdenum trioxide, a nickel compound, and an inorganic oxide material.This highly stable heavy hydrocarbon hydrodesulfurization catalyst maybe made by the method comprising: co-mulling an inorganic oxidematerial, molybdenum trioxide, and a nickel compound to form a mixture;forming said mixture into a particle; and calcining said particle toprovide a calcined mixture. The highly stable heavy hydrocarbonhydrodesulfurization catalyst further may be used in a process for thedesulfurization of a heavy hydrocarbon feedstock, wherein said processcomprises: contacting, under suitable heavy hydrocarbon desulfurizationconditions, a heavy hydrocarbon feedstock with a heavy hydrocarbonhydrodesulfurization catalyst comprising a calcined mixture made bycalcining a formed particle of a mixture comprising molybdenum trioxide,a nickel compound, and an inorganic oxide material; and yielding adesulfurized product.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 presents plots of the P-value of the product yielded from thehydroprocessing of heavy hydrocarbon feedstock when using the inventivecatalyst as compared to a comparison catalyst as a function of pitchconversion. As may be seen from the two plots, the inventive catalystprovides for a product having a higher P-value than that provided by thecomparison catalyst and, thus, a more stable product.

FIG. 2 presents comparison plots of the relative values for thecalculated Weight Average Bed Temperature (WABT) as a function of timefor an 88% hydrodesulfurization of a heavy feedstock using the inventivecatalyst as compared to a comparison catalyst. The slope of the plotsprovide an indication of the stability of the catalyst activity, and therelative positions of the two plots reflects the relative catalyticactivity of the catalysts.

DETAILED DESCRIPTION OF THE INVENTION

A novel catalyst composition has been discovered that is especiallyuseful in the hydrodesulfurization and hydroconversion of heavyhydrocarbon streams that contain sulfur and heavy hydrocarbons having aboiling temperature greater than 538° C. (1000° F.). This catalystcomposition exhibits exceptional stability in its desulfurizationactivity even though it is used at higher process temperature conditionsthan those typically used for hydrodesulfurization in order to providefor high conversion of the heavy hydrocarbons contained in the heavyhydrocarbon stream that is to be processed or treated. Also, thecatalyst composition provides for a hydroconverted and desulfurizedproduct that exhibits high stability in the sense that it has a lowflocculation tendency as compared to hydroconverted products resultingfrom the use of alternative catalysts. Aside from the numerous catalyticand process advantages that the novel catalyst provides, it also has alow cost to produce due to the novel method of making the catalystcomposition.

The inventive catalyst composition comprises a calcined mixture that ismade by calcining a formed particle of a mixture comprising molybdenumtrioxide, a nickel compound, and an inorganic oxide material. It is anessential aspect of the invention for at least a major portion of themolybdenum component of the inventive catalyst to be supplied bymolybdenum trioxide as opposed to precursors of molybdenum trioxide suchas certain of the salts of molybdenum, for example, ammonium dimolybdateand ammonium heptamolybdate. And, indeed, it is an important aspect ofthe invention for the mixture from which the particle is formed is to bemade using molybdenum trioxide. It is preferred for the molybdenumtrioxide used in the formation of the mixture to be in the form of afinely defined powder, which may be in a liquid suspension or slurry.Therefore, the mixture that is formed into a particle and thereaftercalcined can comprise a substantial absence of a molybdenum compoundthat is in a form other than as molybdenum trioxide, such as, forexample, a molybdenum salt compound.

What is meant herein when referring to the substantial absence of amolybdenum compound in a form other than as molybdenum trioxide is thatthe mixture that is shaped or formed into a formed particle andthereafter calcined under suitable calcination conditions, as more fullydescribed elsewhere herein, contains less than a small or less than anegligible amount of a molybdenum compound other than molybdenumtrioxide, such as, for example, a molybdenum salt compound or aninorganic molybdenum compound. Examples of molybdenum compounds otherthan molybdenum trioxide include ammonium molybdate, ammoniumdimolybdate, ammonium heptamolybdate, molybdenum acetate, molybdenumbromide, molybdenum chloride, molybdenum sulfide, and molybdenumcarbide. It is, thus, desirable for the mixture to contain less than 2weight percent, based on the total weight of the mixture, of amolybdenum compound other than molybdenum trioxide. It is preferred forthe mixture to contain less than 1 weight percent of a molybdenumcompound other than molybdenum trioxide, and, most preferred, less than0.5 weight percent.

In another embodiment of the invention, the mixture may consistessentially of molybdenum trioxide, a nickel compound, and an inorganicoxide material. As the phrase “consist essentially of”, or similarphraseology, is used herein in defining the elements or components thatmake up the mixture, what is meant is that a material amount of anymolybdenum compound other than molybdenum trioxide is excluded from themixture. This phrase, however, is not intended to mean that excludedfrom the recited components of the mixture are material amounts of othercompounds such as promoter components including phosphorous compounds. Amaterial amount of a molybdenum compound other than molybdenum trioxideis an amount of such compound contained in the mixture that provides fora material effect upon the catalytic performance properties of the finalcatalyst. These catalyst performance properties are discussed in detailelsewhere herein.

The amount of molybdenum trioxide that is contained in the mixtureshould be such as to provide for the final calcined mixture having amolybdenum content in the range upwardly to 12 weight percent, as metal,(18 wt. % based on MoO₃), with the weight percent being based on thetotal weight of the calcined mixture. However, it is desirable for theamount of molybdenum trioxide that is contained in the mixture to besuch as to provide for the final calcined mixture having a molybdenumcontent in the range of from 4 to 11 wt. %, as metal (6 to 16.5 wt. %,as oxide), but, preferably, from 5 to 10 wt. % (7.5 to 15 wt. %, asoxide), and, most preferably, from 6 to 9 wt. % (9 to 13.5 wt. %, asoxide).

In addition to the molybdenum trioxide component, the mixture furthercontains a nickel compound. The source of the nickel component of themixture is not as critical to the manufacture of the inventive catalystas is the source of the molybdenum component, and, thus, the nickelcomponent may be selected from any suitable nickel compound that iscapable of being mixed with the other components of the mixture and tobe shaped into a particle that is to be calcined to form the finalcalcined mixture. The nickel compounds may include, for example, thenickel hydroxides, nickel nitrates, nickel acetates, and nickel oxides.

The amount of nickel compound that is contained in the mixture should besuch as to provide for the final calcined mixture having a nickelcontent in the range upwardly to 4 weight percent, as metal, (5.1 wt. %based on NiO), with the weight percent being based on the total weightof the calcined mixture. However, it is desirable for the amount of thenickel compound that is contained in the mixture to be such as toprovide for the final calcined mixture having nickel content in therange of from 0.5 to 3.5 wt. %, as metal (0.64 to 4.45 wt. %, as oxide),but, preferably, from 1 to 3 wt. % (1.27 to 3.82 wt. %, as oxide), and,most preferably, from 1.5 to 2.5 wt. % (1.91 to 3.18 wt. %, as oxide).

In addition to the molybdenum trioxide component and the nickelcompound, the mixture further includes an inorganic oxide material. Anysuitable porous inorganic refractory oxide that will provide the surfacestructure properties required for the inventive catalyst may be used asthe inorganic oxide material component of the mixture. Examples ofpossible suitable types of porous inorganic refractory oxides includesilica, alumina, and silica-alumina. Preferred is either alumina orsilica-alumina.

The amount of inorganic oxide material that is contained in the mixtureis such as to provide an amount in the range of from 50 to 95 weightpercent inorganic oxide material in the final calcined mixture with theweight percent being based on the total weight of the calcined mixture.Preferably, the amount of inorganic oxide material in the calcinedmixture is in the range of from 60 to 92 weight percent, and, mostpreferably, from 70 to 89 weight percent.

In addition to the requirement that the source of the molybdenumcomponent of the inventive catalyst is to be predominantly provided bymolybdenum trioxide, the surface characteristics of the inventivecatalyst can also be important to its performance in the hydroconversionand desulfurization of a heavy hydrocarbon feed stream containing aconcentration of sulfur. It is important for the inventive catalyst tohave a mean pore diameter that is within a specific, narrow range and tohave a low macroporosity as hereafter described. In order to provide forthe desired catalytic properties, the mean pore diameter of theinventive catalyst is, generally, in the range of from 85 angstroms (Å)to 100 Å. Preferably, the mean pore diameter is in the range of from 86to 98 angstroms, and, most preferably, from 87 to 97 angstroms.

The inventive catalyst should, in addition to having a mean porediameter that is within the specific and narrow range as discussedabove, also have a low macroporosity where a small percentage of thetotal pore volume of the catalyst is contained within the macropores ofthe inventive catalyst. The term macropore is defined as a catalyst poreof a catalyst composition having a diameter greater than 350 angstroms.It is preferred for the inventive catalyst to have a low macroporositysuch that less than 4.5 percent of the total pore volume is containedwithin its macropores, but, more preferred, is that less than 4 percentof the total pore volume is contained in its macropores, and, mostpreferred, less than 3.5 percent of the total pore volume is containedin its macropores. Also, it is desirable for the pore structure of theinventive catalyst to be such that less than 1 percent of the total porevolume to be contained within its macropores having a diameter greaterthan 1000 angstroms, and it is more desirable that less than 0.9 percentof the total pore volume to be contained within the macropores having adiameter greater than 1000 angstroms, and, most desirable, less than 0.8percent of the total pore volume to be contained within the macroporeshaving a diameter greater than 1000 angstroms

A further important property of the inventive catalyst is for it to havea significantly high surface area. It is the particular combination of asignificantly high surface area in combination with the narrowdistribution of pore diameters and the use of the molybdenum trioxide asthe molybdenum source in the manufacture of the inventive catalyst thatcontributes to many of the important performance properties of theinventive catalyst. It is desirable for the inventive catalyst to have areasonably high surface area that exceeds 230 m²/g. Preferably, thesurface area of the inventive catalyst exceeds 240 m²/g, and, mostpreferably, it exceeds 250 m²/g.

It has been found that the inventive method provides for the novelcatalyst that, as earlier noted, exhibits particularly good propertieswhen it is used in the dual hydrodesulfurization and hydroconversion ofa heavy hydrocarbon stream that contains both a concentration of sulfurand heavy hydrocarbons. While it is not known with certainty, it isbelieved that many of the beneficial catalytic properties of theinventive catalyst are associated with the novel method of manufacturingthe catalyst and, also, in the use of molybdenum trioxide for theprincipal source of the molybdenum component of the catalyst as opposedto the use of alternative molybdenum sources in such manufacturing. Itis surmised that the reason for this is in some way associated withmolybdenum trioxide having acidic and other unique properties such thatwhen it is combined with the alumina it more effectively incorporatesand disperses itself within the alumina matrix. In fact, an examinationof certain scan electron micrographs of the inventive catalyst that hasbeen sulfided suggests that there is a significantly lower degree ofmolybdenum disulfide (MoS₂) slab stacking with the stacks having reducedheights and lengths as compared to alternative molybdenum-containinghydroprocessing catalysts.

The inventive method for making the catalyst of the invention includesthe mixing of the appropriate starting materials to form a mixture thatis formed or agglomerated into particles that are then calcined tothereby provide a calcined mixture. The calcined mixture itself may beused as the highly stable dual hydroconversion and hydrodesulfurizationcatalyst or it may be activated prior to or during its use by any numberof known methods including treatment with hydrogen or with sulfur orsulfur compounds, such as, elemental sulfur, hydrogen sulfide or anorganic sulfur compound.

The first step of the inventive method includes combining the startingmaterials of the catalyst to form a mixture. The essential startingmaterials in the preparation of the mixture include molybdenum trioxidethat is preferably in the form of finely divided particles that may beas a dry powder or as particles in a suspension or slurry, and aninorganic oxide material, such as, inorganic oxide material selectedfrom the group consisting of alumina, silica and alumina-silica. Also, anickel component may further be combined with the molybdenum trioxideand inorganic oxide material in the formation of the mixture. The nickelcomponent may be selected from any suitable source of nickel includingnickel salt compounds, both dry or dissolved in solution, or any othernickel compound including those mentioned above.

The formation of the mixture may be done by any method or means known tothose skilled in the art, including, but not limited to, the use of suchsuitable types of solids-mixing machines as tumblers, stationary shellsor troughs, muller mixers, which are either batch type or continuoustype, and impact mixers, and the use of such suitable types of eitherbatch-wise or continuous mixers for mixing solids and liquids or for theformation of paste-like mixtures that are extrudable. Suitable types ofbatch mixers include, but are not limited to, change-can mixers,stationary-tank mixers, double-arm kneading mixers that are equippedwith any suitable type of mixing blade. Suitable types of continuousmixers include, but are not limited to, single or double screwextruders, trough-and-screw mixers and pug mills.

The mixing of starting materials of the catalyst may be conducted duringany suitable time period necessary to properly homogenize the mixture.Generally, the blending time may be in the range of upwardly to 2 ormore than 3 hours. Typically, the blending time is in the range of from0.1 hours to 3 hours.

The term “co-mulling” is used broadly in this specification to mean thatat least the recited starting materials are mixed together to form amixture of the individual components of the mixture that is preferably asubstantially uniform or homogeneous mixture of the individualcomponents of such mixture. This term is intended to be broad enough inscope to include the mixing of the starting materials so as to yield apaste that exhibits properties making it capable of being extruded orformed into extrudate particles by any of the known extrusion methods.But, also, the term is intended to encompass the mixing of the startingmaterials so as to yield a mixture that is preferably substantiallyhomogeneous and capable of being agglomerated into formed particles,such as, spheroids, pills or tablets, cylinders, irregular extrusions ormerely loosely bound aggregates or clusters, by any of the methods knownto those skilled in the art, including, but not limited to, molding,tableting, pressing, pelletizing, extruding, and tumbling.

As already noted, it is an important aspect of the inventive method forat least a major portion of the molybdenum source of the catalyst to bepredominantly molybdenum trioxide. In the mixing or co-mulling of thestarting materials of the catalyst, it is preferred for the molybdenumtrioxide to be in a finely divided state either as a finely powderedsolid or as fine particles in a suspension or slurry. It is best for theparticle sizes of the particulate molybdenum trioxide used in themanufacture of the catalyst to have a maximum dimension of less than 0.5mm (500 microns, μm), preferably, a maximum dimension of less than 0.15mm (150 μm), more preferably, less than 0.1 mm (100 μm), and, mostpreferably, less than 0.075 mm (75 μm).

While it is not known with certainty, it is believed that it isadvantageous to the invention for the molybdenum trioxide that is usedin the manufacture of the inventive catalyst to be in the form of assmall particles as is practically possible; so, therefore, it is notdesired to have a lower limit on the size of the molybdenum trioxideparticles used in the manufacture of the catalyst. However, it isunderstood that the particle size of the molybdenum trioxide used in themanufacture of the catalyst will generally have a lower limit to itssize of greater than 0.2 microns. Thus, the particle size of themolybdenum trioxide used in the formation of the mixture in themanufacture of the inventive catalyst is preferably in the range of from0.2 to 150 μm, more preferably, from 0.3 to 100 μm, and, mostpreferably, from 0.5 to 75 μm. Typically, the size distribution of themolybdenum trioxide particles, whether in a dry powder or a suspensionor otherwise, is such that at least 50 percent of the particles have amaximum dimension in the range of from 2 to 15 μm.

Once the starting materials of the catalyst are properly mixed andformed into the shaped or formed particles, a drying step mayadvantageously be used for removing certain quantities of water orvolatiles that are included within the mixture or formed particles. Thedrying of the formed particles may be conducted at any suitabletemperature for removing excess water or volatiles, but, preferably, thedrying temperature will be in the range of from about 75° C. to 250° C.The time period for drying the particles is any suitable period of timenecessary to provide for the desired amount of reduction in the volatilecontent of the particles prior to the calcination step.

The dried or undried particles are calcined in the presence of anoxygen-containing fluid, such as air, at a temperature that is suitablefor achieving a desired degree of calcination. Generally, thecalcination temperature is in the range of from 450° C. (842° F.) to760° C. (1400° F.). The temperature conditions at which the particlesare calcined can be important to the control of the pore structure ofthe final calcined mixture. Due to the presence of the molybdenumtrioxide in the formed particles, the calcination temperature requiredto provide for a calcined mixture having the required pore structure ishigher than typical temperatures required to calcine other compositionscontaining inorganic oxide materials, especially those that do notcontain molybdenum trioxide. But, in any event, the temperature at whichthe formed particles are calcined to provide the finally calcinedmixture is controlled so as to provide the finally calcined mixturehaving the pore structure properties as described in detail herein. Thepreferred calcination temperature is in the range of from 510° C. (950°F.) to 730° C. (1346° F.), and, most preferably, from 540° C. (1004° F.)to 705° C. (1301° F.).

The calcined mixture is particularly useful as a high stabilityhydroprocessing catalyst for use in the hydroprocessing of a heavyfeedstock stream that has high pitch and sulfur contents. Prior to itsuse, the calcined mixture may, but is not required to, be sulfided oractivated by any of the methods known to those skilled in the art.Generally, in its use in the hydroprocessing of a hydrocarbon feedstock,the calcined mixture is contained within a reaction zone, such as thatwhich is defined by a reactor vessel, wherein a hydrocarbon feedstock iscontacted with the calcined mixture under suitable hydroprocessingreaction conditions and from which a treated hydrocarbon product isyielded.

The preferred hydrocarbon feedstock of the inventive process is a heavyhydrocarbon feedstock. The heavy hydrocarbon feedstock may be derivedfrom any of the high boiling temperature petroleum cuts such asatmospheric tower gas oils, atmospheric tower bottoms, vacuum tower gasoils, and vacuum tower bottoms or resid. It is a particularly usefulaspect of the inventive process to provide for the hydroprocessing of aheavy hydrocarbon feedstock that can be generally defined as having aboiling temperature at its 5% distillation point, i.e. T(5), thatexceeds 300° C. (572° F.) as determined by using the testing procedureset forth in ASTM D-1160. The invention is more particularly directed tothe hydroprocessing of a heavy hydrocarbon feedstock having a T(5) thatexceeds 315° C. (599° F.) and, even, one that exceeds 340° C. (644° F.).

The heavy hydrocarbon feedstock further may include heavier hydrocarbonsthat have boiling temperatures above 538° C. (1000° F.). These heavierhydrocarbons are referred to herein as pitch, and, as already noted, itis recognized that one of the special features of the inventive catalystor process is that it is particularly effective in the hydroconversionof the pitch content of a heavy hydrocarbon feedstock. The heavyhydrocarbon feedstock may include as little as 10 volume percent pitchor as much as 90 volume percent pitch, but, generally, the amount ofpitch included in the heavy hydrocarbon feedstock is in the range offrom 20 to 80 volume percent. And, more typically, the pitch content inthe heavy hydrocarbon feedstock is in the range of from 30 to 75 volumepercent.

The heavy hydrocarbon feedstock further may include a significantly highsulfur content. One of the special features of the invention is that itprovides for both the desulfurization of the heavy hydrocarbon feedstockand the conversion of the pitch to lighter hydrocarbons having lowerboiling temperatures than those of the pitch hydrocarbons. The sulfurcontent of the heavy hydrocarbon feedstock is primarily in the form oforganic sulfur-containing compounds, which may include, for example,mercaptans, substituted or unsubstituted thiophenes, heterocycliccompounds, or any other type of sulfur-containing compound.

A feature of the invention is that it provides for the desulfurizationof the heavy feedstock that has a significantly high sulfur content,such as a sulfur content greater than 1 weight percent, so as to providefor a treated hydrocarbon product having a reduced sulfur content, suchas a sulfur content of less than 1 weight percent. When referring hereinto the sulfur content of either the heavy hydrocarbon feedstock or thetreated hydrocarbon product, the weight percents are determined by theuse of testing method ASTM D-4294. The inventive process is particularlyuseful in the processing of a heavy hydrocarbon feedstock that has asulfur content exceeding 2 weight percent, and with such a heavyhydrocarbon feedstock, the sulfur content may be in the range of from 2to 8 weight percent. The inventive catalyst and process is especiallyuseful in the processing of a heavy hydrocarbon feedstock having anespecially high sulfur content of exceeding 3 or even 4 weight percentand being in the range of from 3 to 7 weight percent or even from 4 to6.5 weight percent.

The inventive process utilizes the inventive catalyst in thehydroprocessing of the heavy hydrocarbon feedstock to provide for thesimultaneous desulfurization and conversion of pitch to yield thetreated hydrocarbon product having reduced sulfur and pitch contents. Inthis process, the heavy hydrocarbon feedstock is contacted with theinventive catalyst under suitable hydrodesulfurization andhydroconversion process conditions and the treated hydrocarbon productis yielded. The treated hydrocarbon product should have a reduced sulfurcontent that is below that of the heavy hydrocarbon feedstock, such as asulfur content of less than 1 weight percent. It is preferred for thereduced sulfur content of the treated hydrocarbon product to be lessthan 0.8 weight percent, and, most preferably, less than 0.6 weightpercent. It is recognized that the inventive process, however, may havethe capability of effectively desulfurizing the heavy hydrocarbonfeedstock to provide the treated hydrocarbon product having a reducedsulfur content of less than 0.5 and even less than 0.4 weight percent.

The inventive process may further provide for a conversion of a portionof the pitch content of the heavy hydrocarbon feedstock. When referringherein to the conversion of pitch or to pitch conversion or othersimilar terminology, what is meant is that a portion of the hydrocarbonscontained in the heavy hydrocarbon feedstock that has a boilingtemperature exceeding 538° C. (1000° F.) is converted to hydrocarbonshaving a boiling temperature less than 538° C. (1000° F.). In apreferred embodiment of the inventive process, the pitch conversion isgreater than 20 volume percent of the pitch contained in the heavyhydrocarbon feedstock, and, more preferably, the pitch conversionexceeds 30 volume percent. Most preferably, the pitch conversion exceeds40 volume percent of the pitch contained in the heavy hydrocarbonfeedstock. A practical upper limit for the pitch conversion is 90 volumepercent, and, more typically, the upper limit for the pitch conversionis 60 volume percent. Thus, the pitch conversion, for example, may be inthe range of from 20 to 90 volume percent, or from 30 to 60 volumepercent, or from 40 to 60 volume percent.

At higher levels of pitch conversion the treated hydrocarbon productquality tends to suffer. This is believed to be due to the agglomerationof the asphaltene structures contained in the heavy hydrocarbonfeedstock being processed. This agglomeration can, at extremeconditions, result in the separation of the solid fraction from thetreated hydrocarbon product and laying down or deposition of the solidsupon process equipment surfaces. In general, the upper limit of pitchconversion is the point at which product precipitation begins to appear.Various techniques have been used in the petroleum process industry topredict the onset of such precipitation, including proprietary testingmethods and the P-value test as it is more fully described elsewhereherein.

One of the advantages provided by the high pitch conversion of theinventive process is that it results in yielding of the treatedhydrocarbon product having hydrocarbons having boiling temperatures inthe naphtha, distillate (diesel and kerosene), and vacuum gas oiltemperature ranges. These yielded products may be pooled with productstreams made by other refinery process units or they may be furtherprocessed. For instance, the distillate products of the inventiveprocess may undergo further hydroprocessing to yield such products askerosene, aviation fuel and diesel, and the vacuum gas oil product ofthe inventive process may be used as feedstock to a refinery unit suchas a fluid catalytic cracking unit or a hydrocracking unit. Dependingupon the particular market conditions, the distillate fraction yieldedfrom the inventive process can be especially valuable, thus, making ahigher distillate yield, as opposed to higher yields of naphtha andvacuum gas oil, highly desirable.

In addition to providing for a significant conversion of the pitchcontent of the heavy hydrocarbon feedstock, the inventive catalyst andprocess may provide for an incrementally greater yield of distillateproduct than alternative catalysts and processes, and, thus, they canprovide greater economic benefits than other alternatives. The inventiveprocess may further provide for a greater proportion of the pitch of theheavy hydrocarbon feedstock that is converted to hydrocarbons having aboiling temperature less than 538° C. (1000° F.) that is converted tohydrocarbons boiling in the distillate boiling range of from 180° C.(356° F.) to 350° C. (662° F.), or to distillate hydrocarbons. Theinventive process, thus, can provide a treated hydrocarbon product,wherein the proportion of the converted pitch that includes hydrocarbonsboiling in the distillate boiling range exceeds 10 weight percent of theconverted pitch. The inventive process preferably provides a treatedhydrocarbon product that includes a proportion of converted pitch thatincludes hydrocarbons boiling in the distillate boiling range thatexceeds 14 weight percent of the converted pitch, more preferably,exceeding 16 weight percent of the converted pitch, and, mostpreferably, exceeding 18 weight percent of the converted pitch. Thisfeature of the inventive process is particularly beneficial when, incombination with other processing, an ultra low sulfur diesel product ismanufactured. This benefit is due to the high amount of yieldeddistillate product having a relatively low sulfur content which makesfurther severe hydroprocessing to make ultra low sulfur diesel productunnecessary. Mild hydrodesulfurization processing may, however, berequired.

Another feature of the inventive process is that, in addition toproviding for desulfurization and pitch conversion, it can provide for asignificant reduction in the Micro-Carbon Residue (MCR) content of thetreated hydrocarbon product of the process that utilizes the inventivecatalyst. Micro-Carbon Residue content refers to a quantity of carbonresidue remaining after evaporation and pyrolysis of a substrate and isdetermined by the testing method ASTM D4530. In cases when the heavyhydrocarbon feedstock has a significant MCR content, the inventiveprocess can provide for a treated hydrocarbon product having an MCRcontent that is below that of the heavy hydrocarbon feedstock, and, infact, the inventive catalyst can provide for a greater reduction in theMCR content than other prior art catalysts. This enhancement in theability to reduce the MCR content of a feedstock is particularlyadvantageous in those situations when the inventive process is providingfor a treated hydrocarbon product that is to be used, or portionsthereof are to be used, as feedstock to a fluid catalytic cracking (FCC)unit. This benefit is recognized in that the MCR content of an FCCfeedstock can significantly impact the amount of such feedstock that theFCC unit is capable of processing. In general, an FCC unit is able toprocess larger quantities of feedstocks that have low levels of MCRcontent than those feedstocks that have high levels of MCR content.

In the inventive process, the heavy hydrocarbon feedstock may have anMCR value exceeding 6%. The inventive process is particularly useful inthe processing of a heavy hydrocarbon feedstock that has an MCR valueexceeding 8% and even exceeding 10%. The treated hydrocarbon product canhave an MCR value of less than 6%, preferably, less than 5%, and, morepreferably, less than 4%.

One disadvantage from the use of the prior art hydroconversion catalystsin the hydroconversion of heavy hydrocarbon feedstocks is that theresulting product will tend to have a low P-value. The P-value(peptization value) is a numerical value that is an indicator of theflocculation tendency of the asphaltenes contained in a hydrocarbonmixture. The determination of the P-value is the method as described byJ. J. Heithaus in “Measurement and Significance of AsphaltenePeptization”, Journal of Institute of Petroleum, Vol. 48, Number 458,February 1962, pp. 45-53, which publication is incorporated herein byreference.

A high P-value for a hydrocarbon mixture indicates that it is stable anda low P-value for a hydrocarbon mixture indicates that it is not asstable in that there is a greater tendency for precipitation of theasphaltenes contained the hydrocarbon mixture. It is recognized that theP-value of a hydroconverted product tends to decline as the percentageof the pitch component of a heavy hydrocarbon feedstock that isconverted increases, thus, indicating a higher tendency for formingprecipitates. But, it is one of the advantages of the inventive catalystand process that they provide for a high amount of pitch conversionwhile still providing for a treated hydrocarbon product that still hasan acceptably high P-value that exceeds 1.25. The catalyst and processcan provide for a pitch conversion of greater than 30 volume percentwhile still providing for a treated hydrocarbon product having a P-valuegreater than 1.25. It is preferred for the P-value of the treatedhydrocarbon product to exceed 1.5, more preferably, to exceed 1.75, and,most preferably, exceeding 2, when the pitch conversion of the heavyhydrocarbon feedstock that is provided by the inventive catalyst andprocess exceeds 30 volume percent. In some instances, the P-value of theheavy hydrocarbon feedstock may be less than 1.

The calcined mixture (catalyst) of the invention may be employed as apart of any suitable reactor system that provides for the contacting ofthe catalyst with the heavy hydrocarbon feedstock under suitablehydroprocessing conditions that may include the presence of hydrogen andan elevated total pressure and temperature. Such suitable reactionsystems can include fixed catalyst bed systems, ebullating catalyst bedsystems, slurried catalyst systems, and fluidized catalyst bed systems.The preferred reactor system is that which includes a fixed bed of theinventive catalyst contained within a reactor vessel equipped with areactor feed inlet means, such as a feed nozzle, for introducing theheavy hydrocarbon feedstock into the reactor vessel, and a reactoreffluent outlet means, such as an effluent outlet nozzle, forwithdrawing the reactor effluent or the treated hydrocarbon product fromthe reactor vessel.

The inventive process generally operates at a hydroprocessing(hydroconversion and hydrodesulfurization) reaction pressure in therange of from 2298 kPa (300 psig) to 20,684 kPa (3000 psig), preferablyfrom 10,342 kPa (1500 psig) to 17,237 kPa (2500 psig), and, morepreferably, from 12,411 kPa (1800 psig) to 15,513 kPa (2250 psig). Thehydroprocessing reaction temperature is generally in the range of from340° C. (644° F.) to 480° C. (896° F.), preferably, from 360° C. (680°F.) to 455° C. (851° F.), and, most preferably, from 380° C. (716° F.)to 425° C. (797° F.).

The flow rate at which the heavy hydrocarbon feedstock is charged to thereaction zone of the inventive process is generally such as to provide aliquid hourly space velocity (LHSV) in the range of from 0.01 hr to 3hr¹. The term “liquid hourly space velocity”, as used herein, means thenumerical ratio of the rate at which the heavy hydrocarbon feedstock ischarged to the reaction zone of the inventive process in volume per hourdivided by the volume of catalyst contained in the reaction zone towhich the heavy hydrocarbon feedstock is charged. The preferred LHSV isin the range of from 0.05 hr⁻¹ to 2 hr⁻¹, more preferably, from 0.1 hr⁻¹to 1.5 hr⁻¹. and, most preferably, from 0.2 hr⁻¹ to 0.7 hr⁻¹.

It is preferred to charge hydrogen along with the heavy hydrocarbonfeedstock to the reaction zone of the inventive process. In thisinstance, the hydrogen is sometime referred to as hydrogen treat gas.The hydrogen treat gas rate is the amount of hydrogen relative to theamount of heavy hydrocarbon feedstock charged to the reaction zone andgenerally is in the range upwardly to 1781 m³/m³ (10,000 SCF/bbl). It ispreferred for the treat gas rate to be in the range of from 89 m³/m³(500 SCF/bbl) to 1781 m³/m³ (10,000 SCF/bbl), more preferably, from 178m³/m³ (1,000 SCF/bbl) to 1602 m³/m³ (9,000 SCF/bbl), and, mostpreferably, from 356 m³/m³ (2,000 SCF/bbl) to 1425 m³/m³ (8,000SCF/bbl).

The following examples are presented to further illustrate theinvention, but they are not to be construed as limiting the scope of theinvention.

Example I

This Example I describes the preparation of Catalyst A.

Catalyst A

The Catalyst A was prepared by first combining 3209 parts by weight 2%silica interstage alumina, 287 parts by weight nickel nitrate (Ni(NO₃)₂)dissolved in 99 parts by weight deionized water, 269 parts by weightmolybdenum trioxide powder (MoO₃), and 652 parts by weight crushedregenerated Ni/Mo/P hydrotreating catalyst within a Muller mixer alongwith 130 parts by weight 69.9% concentrated nitric acid and 30 grams ofa commercial extrusion aid. A total of 2948 parts by weight of water wasadded to these components during the mixing. The components were mixedfor approximately 40 minutes. The mixture had a pH of 4.08 and an LOI of55.7 weight percent. The mixture was then extruded using 1.3 mm trilobedies to form 1.3 trilobe extrudate particles. The extrudate particleswere then dried in air for a period of several hours at a temperature of100° C.

Aliquot portions of the dried extrudate particles were calcined in aireach for a period of two hours at a temperature of 426° C. (800° F.),566° C. (1050° F.), 677° C. (1250° F.), or 732° C. (1350° F.). The finalcalcined mixture contained 2.2 weight percent nickel metal (2.8 wt. % asNiO), 7.9 weight percent molybdenum metal (11.85 wt. % as MoO₃) and85.45 weight percent 2% silica/alumina. The following Table 1 presentscertain properties of the dried extrudate particles that were calcinedat each of the calcination temperatures. As may be seen from the poreproperties presented in Table 1, the percentage of the total pore volumecontained in the macropores having a pore diameter of 1000 Angstroms andlarger is less than 1 percent.

TABLE 1 Properties of Dried Extrudate for Different CalcinationConditions 426° C. 566° C. 677° C. 732° C. Properties (800° F.) (1050°F.) (1250° F.) (1350° F.) Surface Area, m²/g 332 311 256 133.5 Hg PoreSize Dist. (Angs) less than 70 38.8 28.3 9.8 0.8  70-100 41.2 50.1 48.71.6 100-150 12.2 13.5 31.3 18.3 150-350 5.7 6.0 7.5 66.9 350-1000 1.91.9 2.0 11.1 1000+ 0.2 0.2 0.7 0.3 Total Pore Volume, cc/g 0.551 0.5640.596 0.702 Medium Pore Diameter, 76 81 96 128 Å

Example II Constant Sulfur Conversion Example

This Example II describes one of the methods used in testing thecatalysts described in Example I. This method provided for theprocessing of a feedstock having a significant sulfur concentration toyield a product having specified sulfur concentration. The reactortemperature was adjusted to maintain the fixed sulfur concentration inthe reactor product.

Catalyst A and a commercially available hydrodemetallization catalystwere loaded into a 1.5875 cm (⅝ inch) ID by 127 cm (50 inch) stainlesssteel tube reactor in a stacked bed arrangement with 66.7 volume percentof the bed consisting of Catalyst A placed at the bottom of the catalystbed and 33.3 volume percent of the bed consisting of thehydrodemetallization catalyst placed at the top of the catalyst bed.

The tube reactor was equipped with thermocouples placed in a 0.635 cm (¼inch) thermowell inserted concentrically into the catalyst bed, and thereactor tube was held within a 132 cm (52 inch) long 5-zone furnace witheach of the zones being separately controlled based on a signal from athermocouple.

The catalyst of the stacked catalyst bed was activated by feeding atambient pressure a gas mixture of 5 vol. % H₂S and 95 vol. % H₂ to thereactor at a rate of 1.5 LHSV while incrementally increasing the reactortemperature at a rate of 100° F./hr up to 400° F. The catalyst bed wasmaintained at a temperature of 400° F. for two hours and then thetemperature was incrementally increased at a rate of 100° F./hr to atemperature of 600° F., where it was held for one hour followed again byan incremental increase in the temperature at a rate of 75° F./hr up toa temperature of 700° F., where it was held for two hours before coolingthe catalyst bed temperature down to the ambient temperature. Thecatalyst bed was then pressured with pure hydrogen at 1000 psig, and thetemperature of the catalyst bed was incrementally increased at a rate of100° F./hr to 400° F. The reactor was then charged with feedstock whilethe temperature of the reactor was held at 400° F. for one hour. Thecatalyst bed temperature was then incrementally increased at a rate of50° F./hr up 700° F., from which point the run was started.

The feedstock charged to the reactor was a Middle Eastern long residue.The distillation properties of the feedstock as determined by ASTMMethod D7169 are presented in Table 2. Table 3 presents certain otherproperties of the feedstock.

TABLE 2 Distillation of Feedstock Wt. % Temp, ° C. (° F.) IBP 273 (523) 10 377 (711)  20 427 (801)  30 466 (871)  40 503 (937)  50 543 (1009) 60588 (1090) 70 636 (1177) 80 695 (1283) 90 FBP 737 (1359)

TABLE 3 Other properties of the feedstock Property Value Micro-CarbonResidue (MCR) 12.4 Sulfur (wt %) 4.544 Nickel (ppm) 22 Vanadium (ppm) 751000° F.+ (vol %) 51.3

The feedstock was charged to the reactor along with hydrogen gas. Thereactor was maintained at a pressure of 1900 psig and the feedstock wascharged to the reactor at a rate so as to provide a liquid hourly spacevelocity (LHSV) of 0.33 hr⁻¹ and the hydrogen was charged at a rate of3,000 SCF/bbl. The temperature of the reactor was set so as to provide aproduct having a sulfur content of 0.52 wt. %.

The inventive Catalyst A provides for a product having a significantlyreduced sulfur content over the sulfur content of the feedstockprocessed. The sulfur content of the product was less than 0.6 weightpercent with the hydrodesulfurization activity of the catalyst remainingstable over a significant time period.

Example III

This Example III describes the preparation of Catalyst B.

Catalyst B

The Catalyst B was prepared by first dissolving 252 parts by weight ofNi(NO₃)₂.6H₂O in 87 parts of DI water and heating the solution untilclear. Separately, 281 parts by weight of MoO₃ was combined with 3209parts of alumina (2% silica in 98% alumina) and 639 parts of fresh,crushed and sieved commercial Ni—Mo—P catalyst containing alumina andcombined together in a muller. With the muller running, 2905 parts of DIwater, nickel solution and 19 parts of nitric acid (69.8% concentration)were added to the mull mix. The mixture was mulled for a total of 35minutes. The mixture had a pH of 4.18 and an LOI of 56.6 weight percent.The mixture was then extruded using 1.3 mm trilobe dies to form 1.3trilobe extrudate particles. The extrudate particles were then dried inair for a period of several hours at a temperature of 100° C.

Aliquot portions of the dried extrudate particles were calcined in aireach for a period of two hours at a temperature of 800° F., 1000° F.,and 1200° F. The final calcined mixture contained 2.2 weight percentnickel metal (2.8 wt. % as NiO), 7.9 weight percent molybdenum metal(11.85 wt. % as MoO₂), 0.34% of phosphorus (0.55 wt. % of phosphoruspentaoxide), and 84.8 weight percent 2% silica/alumina. The followingTable 4 presents certain properties of the dried extrudate particlesthat were calcined at each of the calcination temperatures.

TABLE 4 Properties of Dried Extrudate for Different CalcinationConditions 426° C. 538° C. 649° C. Properties (800° F.) (1000° F) (1200°F) Crush Strength, lbs/mm 5.63 5.72 5.03 Water Pore Volume, ml/g 0.630.61 0.64 Hg Pore Size Dist. - Hg <70 A 34.1 24.2 11.2  70-100 A 60.469.3 75.4 100-130 A 2.6 3.2 9.6 130-150 0.6 0.7 0.9 150-180 A 0.8 0.80.8 180-350 A 1.4 1.4 1.6 350 A+ 0.1 0.4 0.5 Medium Pore Diameter, Å 7479 90 Total Pore Volume, Hg, cc/g 0.57 0.60 0.59 Surface Area, m2/g 323315 272

Example IV Constant Reactor Temperature Example

This Example describes one of the methods used in testing the catalystdescribed in Example III. This method provided for the processing of afeedstock having significant sulfur and pitch contents to yield aproduct having reduced sulfur and pitch contents and product liquid thatis stable. The reactor temperature was kept constant in conducting thesereactions and the sulfur content, the pitch content and the productliquid quality were monitored.

A multi-barrel reactor was used to conduct this test. The heating blockcontained four parallel tube reactors each of which was 0.59 inch ID by23.625 inches in length 321 stainless steel tube. A single temperaturecontroller was used to control the heater block, which encased all fourof the reactors. Each of the tube reactors was loaded in a stacked bedarrangement with 30 cm³ of Catalyst B placed at the bottom of thecatalyst bed and 6 cm³ of a commercially available hydrodemetallizationcatalyst placed at the top of the catalyst bed. One of the reactors wasloaded with a commercially available alumina supported nickel andmolybdenum hydrodesulfurization catalyst product of Criterion CatalystCompany designated as RN-650 (Catalyst C) as used in the other runs anda commercial HDM catalyst in the remaining bottom section.

The catalyst of the stacked catalyst bed was activated by feeding atambient pressure a gas mixture of 5 vol. % H₂S and 95 vol. % H₂ to thereactor at a rate of 30 SLPH while incrementally increasing the reactortemperature at a rate of 100° F./hr up to 400° F. The catalyst bed wasmaintained at a temperature of 400° F. for two hours, and, then, thetemperature was incrementally increased at a rate of 100° F./hr to atemperature of 600° F., where it was held for two hours followed againby an incremental increase in the temperature at a rate of 50° F./hr upto a temperature of 700° F., where it was held for two hours beforecooling the catalyst bed temperature of 400° F.

The feedstock charged to the reactor was a Middle Eastern crude. Thedistillation properties of the feedstock as determined by ASTM MethodD7169 are presented in Table 5. Table 6 presents certain otherproperties of the feedstock.

TABLE 5 Distillation of Feedstock Wt. % Temp, ° C. (° F.) IBP 10 351(664)  20 399 (750)  30 437 (819)  40 472 (882)  50 510 (950)  60 554(1029) 70 602 (1116) 80 657 (1215) 90 725 (1337) FBP 733 (1351)

TABLE 6 Other properties of the feedstock Property Value Micro-CarbonResidue (MCR) 11.4 Sulfur (wt %) 4.012 Nickel (ppm) 16.7 Vanadium (ppm)59 1000° F.+ (vol %) 43.5

Feedstock was charged to the reactors along with hydrogen gas. Thereactors were maintained at a pressure of 1900 psig, and the feedstockwas charged to the reactors at a rate so as to provide a liquid hourlyspace velocity (LHSV) of 0.6 hr⁻¹ and the hydrogen was charged at a rateof 3,000 SCF/bbl. The temperatures of the reactors were fixed at 725° F.for approximately a month and then raised to 752° F. for the remainingduration.

Presented in FIG. 1 are plots (the estimated linear function based onexperimental data) of the P-value of product as a function of pitchconversion of the feedstock for the process using the inventive CatalystB and for the comparison Catalyst C. As may be observed from the datapresented in FIG. 1, the inventive Catalyst B provides for a productstability as reflected by the P-value that is significantly higher thancomparison Catalyst C. At both the temperatures of operation, theinventive catalyst provides for a higher pitch conversion and a higherproduct P-value. The comparison catalyst provides for a less stableproduct when pitch conversion approaches 65% than does the inventivecatalyst, which provides for a stable product at a significantly higherpitch conversion.

Example V

This Example V describes the preparation of Catalyst D and a comparisonCatalyst E.

Catalyst D

The Catalyst D was prepared by first combining 4047 parts by weight 2%silica interstage alumina, 378 parts by weight nickel nitrate (Ni(NO₃)₂)dissolved in 138 parts by weight deionized water, and 418 parts byweight molybdenum trioxide powder (MoO₃) within a Muller mixer. A totalof 3807 parts by weight of water was added to these components duringthe mixing. The components were mixed for approximately 45 minutes. Themixture had a pH of 4.75 and an LOI of 59.6 weight percent. The mixturewas then extruded using 1.3 mm trilobe dies to form 1.3 trilobeextrudate particles. The extrudate particles were then dried in air fora period of several hours at a temperature of 100° C.

Aliquot portions of the dried extrudate particles were calcined in aireach for a period of two hours at a temperature of 1000° F., 1250° F.,1300° F., or 1350° F. The final calcined mixture contained 2.2 weightpercent nickel metal (2.8 wt. % as NiO), 7.9 weight percent molybdenummetal (11.85 wt. % as MoO₃) and 85.45 weight percent 2% silica/alumina.The following Table 7 presents certain properties of the dried extrudateparticles that were calcined at a calcination temperature of 1250° F.

TABLE 7 Properties of Dried and Calcined Extrudate Properties 677° C.(1250° F.) Crush Strength, lbs/mm 3.81 Water Pore Volume, ml/g 0.75 HgPore Size Dist. - Hg <70 A 5.5  70-100 A 53.6 100-130 A 33.6 130-150 2.1150-180 A 1.4 180-350 A 2.6 350 A+ 1.2 Medium Pore Diameter, Å 98 TotalPore Volume, Hg, cc/g 0.695 Surface Area, m2/g 261

Catalyst E

The comparison Catalyst E was made by combining 4104 parts of aluminapowder with 127 parts of nickel as nickel hydroxide and mulling briefly.With muller running, added 4104 parts of deionized water were added andmuller mix mulled for 55 minutes. Then, the molybdenum as ammoniumdi-molybdate (i.e. a molybdenum salt) and mulled for additional fiveminutes. The mixture had a pH of 7.23 and an LOI of 59 weight percent.The mixture was then extruded using 1.3 mm trilobe dies to form 1.3trilobe extrudate particles. The extrudate particles were then dried inair for a period of several hours at a temperature of 100° C.

Aliquot portions of the dried extrudate particles were calcined in aireach for a period of two hours at a temperature of 1000° F. and 1200° F.The final calcined mixture contained 2.2 weight percent nickel metal(2.8 wt. % as NiO), 7.9 weight percent molybdenum metal (11.85 wt. % asMoO₃) and 85.35 weight percent alumina. The following Table 8 presentscertain properties of the dried extrudate particles that were calcinedat a calcination temperature of 1250° F.

TABLE 8 Properties of Dried and Calcined Extrudate Properties 649° C.(1200° F.) Crush Strength, lbs/mm 3.57 Water Pore Volume, ml/g 0.87 HgPore Size Dist. <70 A 3.3  70-100 A 29.8 100-130 A 58.9 130-150 2.6150-180 A 1.6 180-350 A 2.3 350 A+ 1.5 Total Pore Volume, cc/g 0.69Medium Pore Diameter, Å 105 BET Surface Area, m2/g 254.1

Example VI Constant Temperature Long-Term Testing

This Example VI describes one of the methods used in testing thecatalysts described in Example V. This method provided for theprocessing of a feedstock having significant sulfur and MCR contents toyield a product having reduced sulfur content. The reactor temperaturewas kept constant in conducting these reactions and the sulfur contentof the product was monitored.

A multi-barrel reactor was used to conduct this test. The heating blockcontained four parallel tube reactors each of which was 0.59 inch ID by23.625 inches in length 321 stainless steel tube. A single temperaturecontroller was used to control the heater block, which encased all fourof the reactors. Each of the tube reactors was loaded in a stacked bedarrangement with 30 cm³ of the catalyst to be test (either Catalyst D orE) placed at the bottom of the catalyst bed and 6 cm³ of a commerciallyavailable hydrodemetallization catalyst placed at the top of thecatalyst bed.

The catalyst of the stacked catalyst bed was activated by feeding atambient pressure a gas mixture of 5 vol. % H₂S and 95 vol. % H₂ to thereactor at a rate of 30 SLPH while incrementally increasing the reactortemperature at a rate of 100° F./hr up to 400° F. The catalyst bed wasmaintained at a temperature of 400° F. for two hours, and, then, thetemperature was incrementally increased at a rate of 100° F./hr to atemperature of 600° F., where it was held for two hours followed againby an incremental increase in the temperature at a rate of 50° F./hr upto a temperature of 700° F., where it was held for two hours beforecooling the catalyst bed temperature of 400° F.

The feedstock charged to the reactor was a Middle Eastern crude. Thedistillation properties of the feedstock as determined by ASTM MethodD7169 are presented in Table 9. Table 10 presents certain otherproperties of the feedstock.

TABLE 9 Distillation of Feedstock Wt. % Temp, ° C. (° F.) IBP 10 351(664)  20 399 (750)  30 437 (819)  40 472 (882)  50 510 (950)  60 554(1029) 70 602 (1116) 80 657 (1215) 90 725 (1337) FBP 733 (1351)

TABLE 10 Other properties of the feedstock Property Value Micro-CarbonResidue (MCR) 11.4 Sulfur (wt %) 4.012 Nickel (ppm) 16.7 Vanadium (ppm)59 1000° F.+ (vol %) 43.5

Feedstock was charged to the reactors along with hydrogen gas. Thereactors were maintained at a pressure of 1900 psig, and the feedstockwas charged to the reactors at a rate so as to provide a liquid hourlyspace velocity (LHSV) of 0.6 hr⁻¹ and the hydrogen was charged at a rateof 3,000 SCF/bbl. The temperatures of the reactors were fixed at either725° F. or 752° F.

Presented in FIG. 2 are plots of the relative values for the calculatedWeight Average Bed Temperature (WABT) that would be required for an 88wt % hydrodesulfurization of the feedstock as a function of run time forthe inventive Catalyst D and the comparison Catalyst E. As may beobserved from the data presented in FIG. 1, the inventive Catalyst Dexhibits catalytic activity over time that is significantly higher thanthe activity of the comparison Catalyst E.

1. A method, comprising: preparing a calcined mixture by calcining amixture, wherein said mixture is prepared by co-mulling particulatemolybdenum trioxide, comprising molybdenum trioxide particles of aparticle size of greater than 0.2 μm and less than 500 μm; inorganicrefractory oxide selected from the group consisting of silica, alumina,and silica-alumina; and a nickel compound to provide said mixture;wherein said mixture comprises less than 2 weight percent, based on thetotal weight of said mixture, of a molybdenum compound other thanmolybdenum trioxide, an amount of molybdenum trioxide so as to provide amolybdenum content in said calcined mixture in the range upwardly to 12weight percent, as metal, with the weight percent being based on thetotal weight of said calcined mixture, an amount of nickel compound soas to provide a nickel content in said calcined mixture in the rangeupwardly to 4 weight percent, as metal, with the weight percent beingbased on the total weight of said calcined mixture, and an amount ofinorganic refractory oxide so as to provide from 50 to 95 weight percentinorganic refractory oxide in said calcined mixture, with the weightpercent being based on the total weight of said calcined mixture.
 2. Amethod as recited in claim 1, further comprising: forming said mixtureinto shaped or formed particles prior to said calcining of said mixture.3. A method as recited in claim 2, wherein said calcining step isconducted at a calcination temperature in the range of from 450° C. to760° C.
 4. A method as recited in claim 3, wherein said particle size isless than 150 μm; wherein said molybdenum content in said calcinedmixture is in the range of from 4 to 11 wt. %; wherein said nickelcontent in said calcined mixture is in the range of from 0.5 to 3.5 wt.%; and wherein said amount of inorganic refractory oxide is in the rangeof from 60 to 92 weight percent of said calcined mixture.
 5. A method asrecited in claim 4, wherein said calcined mixture has a lowmacroporosity such that less than 4.5 percent of the total pore volumeis contained within its macropores; wherein said calcined mixture has amean pore diameter in the range of from 85 angstroms to 100 angstroms;wherein said calcined mixture has a surface area that exceeds 230 m²/g;and wherein less than 1 percent of the total pore volume containedwithin the macropores of said calcined mixture a diameter greater than1000 angstroms.
 6. A method as recited in claim 5, wherein said mixtureconsists essentially of molybdenum trioxide, said nickel compound, andsaid inorganic refractory oxide.
 7. A method as recited in claim 6,wherein said particle size is less than 150 μm; wherein said molybdenumcontent in said calcined mixture is in the range of from 5 to 10 wt. %;wherein said nickel content in said calcined mixture is in the range offrom 1 to 3 wt. %; wherein said amount of inorganic refractory oxidepresent in said calcined mixture is in the range of from 70 to 89 weightpercent; wherein said low macroporosity is such that less than 4 percentof the total pore volume is contained within the macropores of saidcalcined mixture; wherein said mean pore diameter of said calcinedmixture is in the range of from 86 angstroms to 98 angstroms; whereinsaid surface area exceeds 240 m²/g; and wherein less than 0.9 percent ofthe total pore volume of said calcined mixture is contained within itsmacropores having a diameter greater than 1000 angstroms.
 8. Acomposition, comprising: a mixture that has been calcined to provide acalcined mixture, and wherein said mixture consists essentially ofmolybdenum trioxide particles of a particle size of greater than 0.2 μmand less than 500 μm; inorganic refractory oxide selected from the groupconsisting of silica, alumina, and silica-alumina; and a nickelcompound, wherein said mixture comprises less than 2 weight percent,based on the total weight of said mixture, of a molybdenum compoundother than molybdenum trioxide, an amount of molybdenum trioxide so asto provide a molybdenum content in said calcined mixture in the rangeupwardly to 12 weight percent, as metal, with the weight percent beingbased on the total weight of said calcined mixture, an amount of nickelcompound so as to provide a nickel content in said calcined mixture inthe range upwardly to 4 weight percent, as metal, with the weightpercent being based on the total weight of said calcined mixture, and anamount of inorganic refractory oxide so as to provide from 50 to 95weight percent inorganic refractory oxide in said calcined mixture, withthe weight percent being based on the total weight of said calcinedmixture.
 9. A composition as recited in claim 8, wherein said particlesize is less than 150 μm; wherein said molybdenum content in saidcalcined mixture is in the range of from 4 to 11 wt. %; wherein saidnickel content in said calcined mixture is in the range of from 0.5 to3.5 wt. %; and wherein said amount of inorganic refractory oxide is inthe range of from 60 to 92 weight percent of said calcined mixture. 10.A composition as recited in claim 9, wherein said calcined mixture has alow macroporosity such that less than 4.5 percent of the total porevolume is contained within its macropores; wherein said calcined mixturehas a mean pore diameter in the range of from 85 angstroms to 100angstroms; wherein said calcined mixture has a surface area that exceeds230 m²/g; and wherein less than 1 percent of the total pore volumecontained within the macropores of said calcined mixture a diametergreater than 1000 angstroms.
 11. A composition as recited in claim 10,wherein said mixture consists essentially of molybdenum trioxide, saidnickel compound, and said inorganic refractory oxide.
 12. A compositionas recited in claim 11, wherein said particle size is less than 150 μm;wherein said molybdenum content in said calcined mixture is in the rangeof from 5 to 10 wt. %; wherein said nickel content in said calcinedmixture is in the range of from 1 to 3 wt. %; wherein said amount ofinorganic refractory oxide present in said calcined mixture is in therange of from 70 to 89 weight percent; wherein said low macroporosity issuch that less than 4 percent of the total pore volume is containedwithin the macropores of said calcined mixture; wherein said mean porediameter of said calcined mixture is in the range of from 86 angstromsto 98 angstroms; wherein said surface area exceeds 240 m²/g; and whereinless than 0.9 percent of the total pore volume of said calcined mixtureis contained within its macropores having a diameter greater than 1000angstroms.
 13. A process, comprising: contacting a heavy hydrocarbonfeedstock having a T(5) exceeding 300° C., from 10 volume percent to 90volume percent pitch, a sulfur content greater than 1 weight percent,and an MCR value exceeding 6% with a catalyst composition comprisingeither a composition as recited in any one of claims 8 through 12 or acalcined mixture prepared by any of the methods of claims 1 through 7under hydroprocessing conditions so as to provide a treated hydrocarbonproduct having a reduced sulfur content of less than 1 weight percent, aconversion of greater than 20 volume percent of the pitch in said heavyhydrocarbon feedstock, and a reduced MCR value of less than 6%.
 14. Aprocess as recited in claim 13, wherein said heavy hydrocarbon feedstockfurther characterized as having a P-value of less than 1 and saidtreated hydrocarbon product has a P-value exceeding 1.25.
 15. A processas recited in claim 13, wherein said hydroprocessing conditions includea reaction pressure in the range of from 2298 kPa to 20,684 kPa, areaction temperature in the range of from 340° C. to 480° C., and aliquid hourly space velocity (LHSV) in the range of from 0.01 hr⁻¹ to 3hr⁻¹.